Methods and systems of upgrading heavy aromatics stream to petrochemical feedstock

ABSTRACT

Provided here are systems and methods that integrate a hydrodearylation process and a transalkylation process into an aromatic recovery complex. Various other embodiments may be disclosed and claimed.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application is a continuation-in-part application of U.S.application Ser. No. 16/600,285, filed Oct. 11, 2019, which itself is adivisional application of U.S. application Ser. No. 16/388,563, filedApr. 18, 2019 and issued as U.S. Pat. No. 10,508,066 on Dec. 17, 2019,which itself is a continuation-in-part application of U.S. applicationSer. No. 16/032,642, filed on Jul. 11, 2018 and issued as U.S. Pat. No.10,294,172 on May 21, 2019, which is a continuation application of U.S.application Ser. No. 15/435,039, filed on Feb. 16, 2017 and issued asU.S. Pat. No. 10,053,401 on Aug. 21, 2018.

TECHNICAL FIELD

The disclosure relates to methods and systems of upgrading heavyaromatics stream to petrochemical feedstock, and more specifically to acombination of a hydrodearylation unit and a transalkylation unit in anaromatics recovery complex.

BACKGROUND

In an aromatics complex, a variety of process units are used to convertnaphtha or pyrolysis gasoline into benzene, toluene and mixed xylenes,which are basic petrochemical intermediates used for the production ofvarious other chemical products. In order to maximize the production ofbenzene, toluene and mixed xylenes, the feed to an aromatics complex isgenerally limited from C₆ up to C₁₁ compounds. In most aromaticcomplexes, the mixed xylenes are processed within the complex to producethe particular isomer-para-xylene, which can be processed downstream toproduce terephthalic acid. This terephthalic acid is used to makepolyesters, such as polyethylene terephthalate. In order to increase theproduction of benzene and para-xylene, the toluene and C₉ and C₁₀aromatics are processed within the complex through a toluene, C₉, C₁₀transalkylation/toluene disproportionation (TA/TDP) process unit toproduce benzene and xylenes. Any remaining toluene, C₉, and C₁₀aromatics are recycled to extinction. Compounds heavier than C₁₀ aregenerally not processed in the TA/TDP unit, as they tend to cause rapiddeactivation of the catalysts used at the higher temperatures used inthese units, often greater than 400° C.

When para-xylene is recovered from mixed xylenes by a selectiveadsorption process unit in the complex, the C₈ feed to the selectiveadsorption unit is processed to eliminate olefins and alkenyl aromaticssuch as styrene in the feed. Olefinic material can react and occlude thepores of the zeolite adsorbent. The olefinic material is removed bypassing a C₈₊ stream across a clay or acidic catalyst to react olefinsand alkenyl aromatics with another (typically aromatic) molecule,forming heavier compounds (C₁₆₊). These heavier compounds are typicallyremoved from the mixed xylenes by fractionation. The heavy compoundscannot be processed in the TA/TDP unit due to their tendency todeactivate the catalyst and are generally removed from the complex aslower value fuels blend stock. As many of the heavy alkyl aromaticcompounds fractionate with the fractions containing greater than 10carbon atoms, they are not typically sent as feedstock to thetransalkylation unit, and instead are sent to gasoline blending or usedas fuel oil.

SUMMARY

A need has been recognized for the characterization and recovery ofhigher value light aromatics in the range from C₆ to C₁₀ from certainheavy compounds before processing aromatic streams through specializedproduct production units, such as the TA/TDP unit. Embodiments disclosedhere include characterization of the products formed during thetreatment of aromatics streams during processing of hydrocarbons.Certain embodiments include processes for recovery of alkylmono-aromatic compounds. An embodiment of the process for recovery ofalkyl mono-aromatic compounds includes the steps of (a) supplying a feedstream containing C₉₊ compounds from an aromatic complex to a separatorto produce a first product stream containing C₉ and C₁₀ compounds and asecond product stream containing one or more of heavy alkyl aromaticcompounds and alkyl-bridged non-condensed alkyl multi-aromaticcompounds; (b) supplying the first product stream containing C₉ and C₁₀compounds to a transalkylation/toluene disproportionation process unitto yield a third product stream enriched in C₈ compounds; (c) allowing ahydrogen stream and the second product stream to react in presence of acatalyst under specific reaction conditions in a hydrodearylationreactor to yield a fourth product stream containing one or more alkylmono-aromatic compounds and a fifth product stream containing C₁₁₊compounds; and (d) supplying the fourth product stream to the toluenetransalkylation/toluene disproportionation process unit to produce alkylmono-aromatic compounds. In an embodiment, the fourth product stream andthe first product stream containing C₉ and C₁₀ compounds are mixed toform a feed stream for the toluene transalkylation/toluenedisproportionation process unit. The feed stream can be from a xylenererun column of an aromatic recovery process. The feed stream can beundiluted by a solvent. A portion of the hydrogen stream may be suppliedto a catalyst bed in the hydrodearylation reactor to quench the catalystbed. The process can further include supplying the fourth product streamcontaining one or more alkyl mono-aromatic compounds to a separator torecover a benzene-containing stream; and supplying thebenzene-containing stream to the toluene transalkylation/toluenedisproportionation process unit to produce alkyl mono-aromaticcompounds. The process can further include recovering a C₈ stream fromthe separator; and supplying the C₈ stream to a para-xylene unit toproduce para-xylene. The process can further include recovering a C₉₊stream from the separator; and supplying the C₉₊ stream to the toluenetransalkylation/toluene disproportionation process unit to produce alkylmono-aromatic compounds. The process can further include supplying thefourth product stream containing one or more alkyl mono-aromaticcompounds to a separator to recover a toluene-containing stream; andsupplying the toluene-containing stream to the toluenetransalkylation/toluene disproportionation process unit to produce alkylmono-aromatic compounds.

The catalyst in the hydrodearylation reactor can include a support madeof one or more of silica, alumina, titania, and a combination thereof.The catalyst in the hydrodearylation reactor can further include anacidic component being at least one member of the group consisting ofamorphous silica-alumina, zeolite, and combinations thereof. The zeolitecan be one or more of or derived from FAU, *BEA, MOR, MFI, or MWWframework types, wherein each of these codes correspond to a zeolitestructure present in the database of zeolite structures as maintained bythe Structure Commission of the International Zeolite Association. Thecatalyst in the hydrodearylation reactor can include an IUPAC Group 6-10metal that is at least one member of the group consisting of iron,cobalt, nickel, molybdenum, tungsten, and combinations thereof. TheIUPAC Group 8-10 metal can be present ranging from 2 to 20 percent byweight of the catalyst and the IUPAC Group 6 metal can be presentranging from 1 to 25 percent by weight of the catalyst. The conditionsin the hydrodearylation reactor can include an operating temperature inthe range of about 200 to 450° C., or about 250 to 450° C. and anoperating hydrogen partial pressure in the range of about 5 bar gauge to100 bar gauge. One of the alkyl mono-aromatic compounds produced by thetoluene transalkylation/toluene disproportionation is a para-xylene.

In some embodiments of the presently disclosed systems and methods,catalysts in addition to or alternative to catalyst supports, such assilica or zeolite catalysts and catalyst supports can contain 0 wt. %added metal catalyst, or a zeolite support system such as silica with analumina binder contains 0 wt. % added metal catalyst. The catalyst inthe hydrodearylation reactor can include an IUPAC Group 6-10 metal thatis at least one member of the group consisting of iron, cobalt, nickel,molybdenum, tungsten, and combinations thereof. An IUPAC Group 8-10metal can be present ranging from about 0 to 20 percent by weight of thecatalyst and an IUPAC Group 6 metal can be present ranging from about 0to 25 percent by weight of the catalyst. In some embodiments of thecatalyst or a catalyst support no metal is present, but in others one ormore metals are present. The conditions in the hydrodearylation reactorcan include an operating temperature in the range of about 200 to 450°C., or about 250 to 450° C. and an operating hydrogen partial pressurein the range of about 5 bar gauge to 100 bar gauge. One of the alkylmono-aromatic compounds produced by the toluene transalkylation/toluenedisproportionation is a para-xylene.

In some embodiments, hydrocracking catalysts containing about 4 wt. %NiO and about 16 wt. % MoO₃ on Ti and Zr modified USY zeolite (10 wt. %)with a silica alumina binder (90 wt. %) can be used. However, in someembodiments only zeolite or only zeolite and a binder can beadvantageously used to function as a hydrodearylation catalyst, withoutadded catalytic metals such as IUPAC Group 6-10 metals.

Certain embodiments include systems for recovery of alkyl mono-aromaticcompounds. An embodiment of a system for conversion of alkyl-bridgednon-condensed alkyl multi-aromatic compounds to alkyl mono-aromaticcompounds includes the following components: (i) a first separatoradapted to receive a feed stream containing one or more of heavy alkylaromatic compounds and one or more alkyl-bridged non-condensed alkylmulti-aromatic compounds having at least two benzene rings connected byan alkyl bridge group with at least two carbons and the benzene ringsbeing connected to different carbons of the alkyl bridge group, andproduces a first product stream containing C₉ and C₁₀ compounds and asecond product stream containing one or more of heavy alkyl aromaticcompounds and alkyl-bridged non-condensed alkyl multi-aromaticcompounds; (ii) a hydrodearylation reactor fluidly coupled to the firstseparator and adapted to receive a hydrogen stream and the secondproduct stream and to produce a third product stream in presence of acatalyst, the third product stream containing one or more alkylmono-aromatic compounds; and (iii) a second separator fluidly coupled tothe hydrodearylation reactor and adapted to receive the third productstream and to produce a benzene-containing stream, a toluene-containingstream, a C₈-rich stream, and a bottoms C₉₊ stream. The system can alsoinclude a transalkylation unit fluidly coupled to the second separatorand adapted to receive the first product stream and one or more of thebenzene-containing stream, the toluene-containing stream, and thebottoms C₉₊ stream, and to produce alkyl mono-aromatic compounds. Thesystem can also include a para-xylene unit fluidly coupled to the secondseparator and adapted to receive the C₈-rich stream and to produce apara-xylene-rich stream.

BRIEF DESCRIPTION OF THE DRAWINGS

Embodiments will be readily understood by the following detaileddescription in conjunction with the accompanying drawings. Embodimentsare illustrated by way of example and not by way of limitation inaccompanying drawings.

FIG. 1 is a schematic representation of certain components of anaromatics processing system that upgrades fuel oil to a petrochemicalfeedstock, according to an exemplary embodiment.

FIG. 2 is a schematic representation of certain components of anaromatics processing system that upgrades fuel oil to a petrochemicalfeedstock, according to an exemplary embodiment.

FIG. 3 is a schematic representation of certain components of anaromatics processing system that upgrades fuel oil to a petrochemicalfeedstock, according to an exemplary embodiment.

FIG. 4 is a schematic representation of certain components of anaromatics processing system that upgrades fuel oil to a petrochemicalfeedstock, according to an exemplary embodiment.

DETAILED DESCRIPTION

The present disclosure describes various embodiments related toprocesses, devices, and systems for conversion of alkyl-bridgednon-condensed alkyl aromatic compounds to alkyl mono-aromatic compounds.Further embodiments are described and disclosed.

In the following description, numerous details are set forth in order toprovide a thorough understanding of the various embodiments. In otherinstances, well-known processes, devices, and systems may not have beendescribed in particular detail in order not to unnecessarily obscure thevarious embodiments. Additionally, illustrations of the variousembodiments may omit certain features or details in order to not obscurethe various embodiments. Here, reference is made to the accompanyingdrawings that form a part of this disclosure. The drawings may providean illustration of some of the various embodiments in which the subjectmatter of the present disclosure may be practiced. Other embodiments maybe utilized, and logical changes may be made without departing from thescope of this disclosure. Therefore, the following detailed descriptionis not to be taken in a limiting sense.

The description may use the phrases “in some embodiments,” “in variousembodiments,” “in an embodiment,” or “in embodiments,” which may eachrefer to one or more of the same or different embodiments. Furthermore,the terms “comprising,” “including,” “having,” and the like, as usedwith respect to embodiments of the present disclosure, are synonymous.

As used in this disclosure, the term “hydrodearylation” refers to aprocess for cleaving of the alkyl bridge of non-condensed alkyl-bridgedmulti-aromatics or heavy alkyl aromatic compounds to form alkylmono-aromatics, in the presence a catalyst and hydrogen.

As used in this disclosure, the term “stream” (and variations of thisterm, such as hydrocarbon stream, feed stream, product stream, and thelike) may include one or more of various hydrocarbon compounds, such asstraight chain, branched or cyclical alkanes, alkenes, alkadienes,alkynes, alkyl aromatics, alkenyl aromatics, condensed and non-condenseddi-, tri- and tetra-aromatics, and gases such as hydrogen and methane,C₂₊ hydrocarbons and further may include various impurities.

As used in this disclosure, the term “zone” refers to an area includingone or more equipment, or one or more sub-zones. Equipment may includeone or more reactors or reactor vessels, heaters, heat exchangers,pipes, pumps, compressors, and controllers. Additionally, an equipment,such as reactor, dryer, or vessels, further may include one or morezones.

As used in this disclosure, the term “rich” means an amount of at least30% or greater, by mole percentage of a compound or class of compoundsin a stream. Certain streams rich in a compound or class of compoundscan contain about 50% or greater, by mole percentage of the particularcompound or class of compounds in the streams. In certain cases, molepercentage may be replaced by weight percentage, in accordance withstandard industry usage.

As used in this disclosure, the term “mixed xylenes” refers to a mixturecontaining one or more C₈ aromatics, including any one of the threeisomers of di-methylbenzene and ethylbenzene. As used in thisdisclosure, the term “conversion” refers to the conversion of compoundscontaining multiple aromatic rings or mono-aromatic compounds with heavy(C₄₊) alkyl groups boiling above 210° C. to mono-aromatic compounds witha lighter alkyl groups boiling below 210° C.

During hydrocarbon processing, compounds composed of an aromatic ringwith one or more coupled alkyl groups containing three or more carbonmolecules per alkyl group are formed. Formation of these compounds maybe from processes used by petroleum refiners and petrochemical producersto produce aromatic compounds from non-aromatic hydrocarbons, such ascatalytic reforming. As many of these heavy alkyl aromatic compoundsfractionate with the fractions containing greater than 10 carbon atoms,they are not typically sent as feedstock to the transalkylation unit,and instead are sent to gasoline blending or used as fuel oil. Themethods and systems disclosed here result in upgrading a low-value fueloil to petrochemical feed.

Provided here is an embodiment of a process to fractionate an effluentstream of a xylene re-run column and supply it as a feed stream to ahydrodearylation unit. In an embodiment, this stream is eithersubsequently processed or used to upgrade the fuel oil components (heavyfraction) to petrochemical feedstock. Methods and system disclosed herecreate value by processing a reject/bottoms stream from an aromaticcomplex and by upgrading a significant proportion of fuel oil intopetrochemical feedstock. In an embodiment, the C₉₊ stream from a xylenere-run column is fractionated to remove C₉ and C₁₀, leaving a C₁₁₊stream, which is considered as a low-value fuel oil stream. The C₉ andC₁₀ stream is directed to a TA/TDP process unit to yield increasedquantities of C₈ that can be further processed downstream to yieldpara-xylene. The C₁₁₊ fuel oil stream is subjected to hydrodearylationand the hydrodearylated liquid products sent for processing in atransalkylation unit. The unconverted C₁₁₊ (mainly condenseddiaromatics) stream is directed as fuel oil.

Disclosed here is a process for recovery of alkyl mono-aromaticcompounds that includes the following steps. A feed stream containingC₉₊ compounds from an aromatic complex is supplied to a separator toproduce a first product stream containing C₉ and C₁₀ compounds and asecond product stream containing one or more of heavy alkyl aromaticcompounds and alkyl-bridged non-condensed alkyl multi-aromaticcompounds. In an embodiment, the feed stream is from a xylene reruncolumn of an aromatic recovery process. In certain embodiments, the feedstream is undiluted by solvents and is directly supplied to theseparator. In an embodiment, the second product stream contains C₁₁₊compounds. This first product stream containing C₉ and C₁₀ compounds issupplied to a TA/TDP process unit to yield a third product streamenriched in C₈ compounds. The second product stream and a hydrogenstream are supplied to a hydrodearylation reactor to react in presenceof a catalyst under specific reaction conditions to yield a fourthproduct stream containing C₉ and C₁₀ compounds and a fifth productstream containing unconverted C₁₁₊ compounds. The fourth product streamis supplied further to a TA/TDP process unit to supply and produce alkylmono-aromatic compounds. In certain embodiments, the C₈ content in thefourth product stream increases following the processing in the TA/TDPprocess unit. In certain embodiments, the fifth product streamcontaining unconverted C₁₁₊ compounds can be recycled to thehydrodearylation reactor. In certain embodiments, the fourth productstream and the first product stream containing C₉ and C₁₀ compounds aremixed to form a feed stream for the TA/TDP process unit. In certainembodiments, the alkyl mono-aromatic compounds produced by the TA/TDPprocess unit is para-xylene. In certain embodiments, the hydrodearylatedproducts are supplied to a separator to recover a benzene-containingstream. And this benzene-containing stream can be directed to anappropriate part of the TA/TPD process unit. In certain embodiments, thehydrodearylated products are supplied to a separator to recover atoluene-containing stream. And this toluene-containing stream can bedirected to an appropriate part of the TA/TPD process unit.

In an embodiment, the feedstock to the hydrodearylation reactor (eitherwhole or fractionated) is mixed with an excess of hydrogen gas in amixing zone. A portion of the hydrogen gas is mixed with the feedstockto produce a hydrogen-enriched liquid hydrocarbon feedstock. Thishydrogen-enriched liquid hydrocarbon feedstock and undissolved hydrogenis supplied to a flashing zone in which at least a portion ofundissolved hydrogen is flashed, and the hydrogen is recovered andrecycled. The hydrogen-enriched liquid hydrocarbon feedstock from theflashing zone is supplied as a feed stream to the hydrodearylationreactor. The hydrodearylated liquid product stream that is recoveredfrom the hydrodearylation reactor is further processed as provided here.

In certain embodiments, the hydrogen stream is combined with the secondproduct stream before being supplied to the hydrodearylation reactor. Incertain embodiments, the hydrogen stream includes a recycled hydrogenstream and a makeup hydrogen stream. In certain embodiments, thehydrogen stream comprises at least 70% hydrogen by weight. The catalystcan be presented as a catalyst bed in the reactor. In certainembodiments, a portion of the hydrogen stream is fed to the catalyst bedin the reactor to quench the catalyst bed. In certain embodiments, thecatalyst bed is comprised of two or more catalyst beds. The catalyst caninclude a support that is at least one member of the group consisting ofsilica, alumina, titania, and combinations thereof, and further includesan acidic component that is at least one member of the group consistingof amorphous silica-alumina, zeolite, and combinations thereof. Thezeolite can be one or more of or derived from FAU, *BEA, MOR, MFI, orMWW framework types, wherein each of these codes correspond to a zeolitestructure present in the database of zeolite structures as maintained bythe Structure Commission of the International Zeolite Association. Incertain embodiments, the catalyst includes an IUPAC Group 8-10 metal andan IUPAC Group 6 metal. In certain embodiments, the catalyst includes anIUPAC Group 8-10 metal that is at least one member of the groupconsisting of iron, cobalt, and nickel, and combinations thereof. Thecatalyst includes an IUPAC Group 6 metal that is at least one member ofthe group consisting of molybdenum and tungsten, and combinationsthereof. In certain embodiments, the IUPAC Group 8-10 metal is 2 to 20percent by weight of the catalyst and the IUPAC Group 6 metal is 1 to 25percent by weight of the catalyst. In certain embodiments, the catalystis comprised of nickel, molybdenum, ultrastable Y-type zeolite, andsilica-alumina support.

In some embodiments of the presently disclosed systems and methods,catalysts in addition to or alternative to catalyst supports, such assilica or zeolite catalysts and catalyst supports can contain 0 wt. %added metal catalyst, or a zeolite support system such as silica with analumina binder contains 0 wt. % added metal catalyst. The catalyst inthe hydrodearylation reactor can include an IUPAC Group 6-10 metal thatis at least one member of the group consisting of iron, cobalt, nickel,molybdenum, tungsten, and combinations thereof. An IUPAC Group 8-10metal can be present ranging from about 0 to 20 percent by weight of thecatalyst and an IUPAC Group 6 metal can be present ranging from about 0to 25 percent by weight of the catalyst. In some embodiments of thecatalyst or a catalyst support no metal is present, but in others one ormore metals are present. The conditions in the hydrodearylation reactorcan include an operating temperature in the range of about 200 to 450°C., or about 250 to 450° C. and an operating hydrogen partial pressurein the range of about 5 bar gauge to 100 bar gauge. One of the alkylmono-aromatic compounds produced by the toluene transalkylation/toluenedisproportionation is a para-xylene.

In some embodiments, hydrocracking catalysts containing about 4 wt. %NiO and about 16 wt. % MoO₃. on Ti and Zr modified USY zeolite (10 wt.%) with a silica alumina binder (90 wt. %) can be used. However, in someembodiments only zeolite or only zeolite and a binder can beadvantageously used to function as a hydrodearylation catalyst, withoutadded catalytic metals such as IUPAC Group 6-10 metals.

In certain embodiments, the specific reaction conditions include anoperating temperature of the reactor during the hydrodearylationreaction that is in the range of 200 to 450° C. In certain embodiments,the specific reaction conditions include an operating temperature of thereactor during the hydrodearylation reaction that is in the range of 250to 350° C. In certain embodiments, the specific reaction conditionsinclude an operating temperature of the reactor during thehydrodearylation reaction that is in the range of 300 to 350° C. Thespecific reaction conditions can include a hydrogen partial pressure ofthe reactor during the hydrodearylation reaction that is in the range of5 to 100 bar gauge. In certain embodiments, the specific reactionconditions can include a hydrogen partial pressure of the reactor duringthe hydrodearylation reaction that is in the range of 50 to 100 bargauge. In certain embodiments, the specific reaction conditions caninclude a hydrogen partial pressure of the reactor during thehydrodearylation reaction that is in the range of 5 to 80 bar gauge. Incertain embodiments, the specific reaction conditions can include ahydrogen partial pressure of the reactor during the hydrodearylationreaction that is in the range of 5 to 30 bar gauge. The hydrogen partialpressure of the reactor during the hydrodearylation reaction can bemaintained at less than 20 bar gauge. The specific reaction conditionscan include a feed rate of the hydrogen stream that is in the range of100 to 1000 standard liter per liter of feedstock. The specific reactionconditions can include a feed rate of the hydrogen stream that is in therange of 100 to 300 standard liter per liter of feedstock.

In an embodiment, a system is provided for conversion of alkyl-bridgednon-condensed alkyl multi-aromatic compounds to alkyl mono-aromaticcompounds. The system includes (i) a first separator that receives afeed stream containing one or more of heavy alkyl aromatic compounds andone or more alkyl-bridged non-condensed alkyl multi-aromatic compoundshaving at least two benzene rings connected by an alkyl bridge groupwith at least two carbons and the benzene rings that is connected todifferent carbons of the alkyl bridge group, and produces a firstproduct stream containing C₉ and C₁₀ compounds and a second productstream containing one or more of heavy alkyl aromatic compounds andalkyl-bridged non-condensed alkyl multi-aromatic compounds; (ii) ahydrodearylation reactor fluidly coupled to the first separator andadapted to receive a hydrogen stream and the second product stream andto produce a third product stream in presence of a catalyst, and thethird product stream containing one or more alkyl mono-aromaticcompounds; (iii) a second separator fluidly coupled to thehydrodearylation reactor and adapted to receive the third product streamand to produce a benzene-containing stream, a toluene-containing stream,a C₈-rich stream, and a bottoms C₉₊ stream. In certain embodiments, thesystem further includes a transalkylation unit that is adapted toreceive the toluene-containing stream and the bottoms C₉₊ stream and toproduce alkyl mono-aromatic compounds. In order to increase theproduction of benzene and para-xylene, the toluene and C₉ and C₁₀aromatics are processed within the complex through a toluene, C₉, C₁₀transalkylation/toluene disproportionation (TA/TDP) process unit toproduce benzene and xylenes. Any remaining toluene, C₉, and C₁₀aromatics are recycled to extinction. In certain embodiments, the secondproduct stream is a C₁₁₊ stream. In certain embodiments, the alkylmono-aromatic compounds produced by the transalkylation unit includespara-xylene.

A typical refinery with an aromatic complex contains the followingunits: an atmospheric distillation unit, a diesel hydrotreating unit, anatmospheric residue unit, a naphtha hydrotreating unit, a naphthareforming unit and an aromatics complex. The whole crude oil isdistilled in an atmospheric distillation column to recover a naphthafraction (compounds with a boiling point ranging from 36° C. to 180°C.), diesel fraction (compounds with a boiling point ranging from 180°C. to 370° C.) and atmospheric residue fraction (compounds with aboiling point at 370° C. or higher). The naphtha fraction ishydrotreated in a naphtha hydrotreating unit to reduce the sulfur andnitrogen content to less than 0.5 part per million by weight and thehydrotreated naphtha fraction is sent to a catalytic reforming unit toimprove its quality, such as, an increase in the octane number toproduce gasoline blending stream or feedstock for an aromatics recoveryunit. Similarly, the diesel fraction is hydrotreated in a separatehydrotreating unit to desulfurize the diesel oil to obtain dieselfraction meeting the stringent specifications of sulfur content that isless than 10 parts per million. The atmospheric residue fraction iseither used a fuel oil component or sent to other separation/conversionunits to convert low value hydrocarbons to high value products. Thereformate fraction from the catalytic reforming unit can be used asgasoline blending component or sent to an aromatic complex to recoverhigh value aromatics, such as, benzene, toluene, and xylenes. Thereformate fraction from catalytic reforming unit is split into twofractions: light and heavy reformate. The light reformate is sent to abenzene extraction unit to extract the benzene and recover gasoline thatis substantially free of benzene. The heavy reformate stream is sent toa para-xylene (p-xylene) extraction unit to recover p-xylene. Otherxylenes that are recovered from the p-xylene unit are sent to a xyleneisomerization unit to convert them to p-xylene. The converted fractionis recycled to the p-xylene extraction unit. The heavy fraction from thep-xylene extraction unit is recovered as a process reject or bottomsstream. The aromatics bottoms fraction from an aromatic recovery complexis processed in two ways. One, the aromatics bottoms fraction isfractionated into a 180-° C. fraction ((compounds with a boiling pointless than 180° C.) and sent to a gasoline pool as blending components,and a 180+° C. fraction sent to a hydrodearylation unit. Alternatively,the aromatics bottoms fraction is sent directly to a hydrodearylationunit to recover light alkyl mono-aromatic compounds from heavy alkylaromatic and alkyl-bridged non-condensed alkyl aromatic compounds. Atypical system for aromatic transalkylation to ethylbenzene and xylenesincludes the following components: a first transalkylation reactor, aseries of separators, a second transalkylation reactor, a stabilizer,and a p-xylene production unit. The feed stream to the firsttransalkylation reactor is a mixture of a C₉₊ alkyl aromatics mixtureand benzene. This feed stream in brought into contact with a zeolitecatalyst in the first transalkylation reactor. The effluent stream fromthis transalkylation reactor is directed to a separation column. Thiseffluent stream may be combined with effluent streams from the secondtransalkylation reactor before entry into a separation column. There arethree exit streams from the separation column: an overhead streamcontaining benzene, a bottoms stream of C₈₊ aromatics includingethylbenzene and xylenes, and a side-cut stream containing toluene. Theoverhead stream is recycled to the first transalkylation reactor. Thebottoms stream is supplied to a second separation column. An overheadstream containing ethylbenzene and xylenes from the second separationcolumn is directed to a para-xylene unit to produce a para-xyleneproduct stream and a bottoms stream of C₉₊ alkylaromatics. The side-cutstream from the separation column is recycled to a secondtransalkylation unit with or without the recovery of toluene. Thisside-cut stream from the separation column can be combined with bottomsstream from second separation column to form a combined stream that issupplied to a third separation column. This separation column separatesthe combined stream into a bottoms stream of C₁₁₊ alkylaromatics(“heavies”) and an overhead stream of C₉, C₁₀ alkylaromatics, andlighter compounds (including C₇ alkylaromatics) directed to a secondtransalkylation unit. Hydrogen is also supplied to the secondtransalkylation unit. Here, in the second transalkylation unit, theoverhead stream and hydrogen are brought in contact with atransalkylation catalyst, and the effluent stream is directed to astabilizer column. Two streams exit the stabilizer column: an overheadstream of light end hydrocarbons (generally comprising at least ethane)and a bottom stream of a second transalkylation product.

As previously described, the aromatic bottoms stream from an aromaticrecovery complex can be directly supplied to a hydrodearylation unit anda hydrodearylated liquid product stream can be recovered for furtherprocessing. In an embodiment 100 as described in FIG. 1, the aromaticbottoms stream 104 from an aromatic recovery complex 102 is sent to aseparator 106. In an embodiment, this separator 106 can be a separationunit including a distillation column with 5 or more theoretical trays.In an embodiment, the separator 106 can be a flash vessel or a stripper.Two streams exit the separator 106: an overhead stream 108 containing C₉and C₁₀ compounds and a bottoms stream 110 containing C₁₁₊ compounds. Inan embodiment, the overhead stream 108 contains about 50-99 wt. % of theC₉ and C₁₀ compounds. In another embodiment, the overhead stream 108contains about 60-99 wt. % of the C₉ and C₁₀ compounds. In anembodiment, the overhead stream 108 contains about 80-99 wt. % of the C₉and C₁₀ compounds. For example, simulated distillation data indicatedthat the overhead stream 108 contains about 90-99 wt. % of the C₉ andC₁₀ compounds. And this data aligned with the two-dimensional gaschromatography data obtained in this instance, which revealed the stream104 as containing about 91 wt. % of the C₉ and C₁₀ compounds. The C₉₊feed from a refinery can be “heavy” with a different composition. Inother instances, the C₉ and C₁₀ compounds made up about 68 wt. % of thefeed as determined by two-dimensional gas chromatography. The bottomsstream 110 containing C₁₁₊ compounds is directed to a hydrodearylationunit 112 for processing into a hydrodearylated liquid product stream114. In an embodiment, the bottoms stream 110 contains about 5-99 wt. %of C₁₁₊ compounds. In another embodiment, the bottoms stream 110contains about 30-99 wt. % of C₁₁₊ compounds. In an embodiment, thebottoms stream 110 contains about 80-99 wt. % of C₁₁₊ compounds. In anembodiment, the hydrodearylated liquid product stream 114 containsgreater than 10 wt. % of alkyl mono-aromatic compounds. In anembodiment, the hydrodearylated liquid product stream 114 containsgreater than 20 wt. % of alkyl mono-aromatic compounds. In anembodiment, the hydrodearylated liquid product stream 114 containsgreater than 40 wt. % of alkyl mono-aromatic compounds. In anembodiment, the hydrodearylated liquid product stream 114 contains about50 wt. % of alkyl mono-aromatic compounds. In an embodiment, thehydrodearylated liquid product stream 114 contains about 70 wt. % ofalkyl mono-aromatic compounds. In an embodiment, the hydrodearylatedliquid product stream 114 contains about 90 wt. % of alkyl mono-aromaticcompounds. In an embodiment, the hydrodearylated liquid product stream114 contains less than 70 wt. % of di-aromatic compounds. In anembodiment, the hydrodearylated liquid product stream 114 contains lessthan 50 wt. % of di-aromatic compounds. In an embodiment, thehydrodearylated liquid product stream 114 contains less than 40 wt. % ofdi-aromatic compounds. In an embodiment, the hydrodearylated liquidproduct stream 114 contains less than 20 wt. % of di-aromatic compounds.In an embodiment, the hydrodearylated liquid product stream 114 containsless than 10 wt. % of di-aromatic compounds. In an embodiment, thehydrodearylated liquid product stream 114 contains less than 1 wt. % ofdi-aromatic compounds. The overhead stream 108 containing C₉ and C₁₀compounds is combined with the hydrodearylated liquid product stream 114leaving the hydrodearylation unit, and this combined stream 116 issupplied to a transalkylation reactor for further processing.

In another embodiment, the aromatic bottoms stream from an aromaticrecovery complex is sent to a separator. In an embodiment, thisseparator can be a separation unit including a distillation column with5 or more theoretical trays. In an embodiment, the separator can be aflash vessel or a stripper. In an embodiment 200 as described in FIG. 2,the aromatic bottoms stream 204 from an aromatic recovery complex 202 issent to a first separator 206. Two streams exit the first separator 206:an overhead stream 208 containing C₉ and C₁₀ compounds and a bottomsstream 210 containing C₁₁₊ compounds. In an embodiment, the overheadstream 208 contains about 50-99 wt. % of the C₉ and C₁₀ compounds. Inanother embodiment, the overhead stream 208 contains about 60-99 wt. %of the C₉ and C₁₀ compounds. In an embodiment, the overhead stream 208contains about 80-99 wt. % of the C₉ and C₁₀ compounds. In anembodiment, the overhead stream 208 contains about 90-99 wt. % of the C₉and C₁₀ compounds. The bottoms stream 210 containing C₁₁₊ compounds isdirected to a hydrodearylation unit 212 for processing a hydrodearylatedliquid product stream 214. In an embodiment, the bottoms stream 210contains about 5-99 wt. % of C₁₁₊ compounds. In another embodiment, thebottoms stream 210 contains about 30-99 wt. % of C₁₁₊ compounds. In anembodiment, the bottoms stream 210 contains about 80-99 wt. % of C₁₁₊compounds. The hydrodearylated liquid product stream 214 is supplied toa second separator 216. In an embodiment, the hydrodearylated liquidproduct stream 214 contains about 10 wt. % of alkyl mono-aromaticcompounds. In an embodiment, the hydrodearylated liquid product stream214 contains about 20 wt. % of alkyl mono-aromatic compounds. In anembodiment, the hydrodearylated liquid product stream 214 contains about40 wt. % of alkyl mono-aromatic compounds. In an embodiment, thehydrodearylated liquid product stream 214 contains about 50 wt. % ofalkyl mono-aromatic compounds. In an embodiment, the hydrodearylatedliquid product stream 214 contains about 70 wt. % of alkyl mono-aromaticcompounds. In an embodiment, the hydrodearylated liquid product stream214 contains about 90 wt. % of alkyl mono-aromatic compounds. In anembodiment, the hydrodearylated liquid product stream 214 contains lessthan 70 wt. % of di-aromatic compounds. In an embodiment, thehydrodearylated liquid product stream 214 contains less than 40 wt. % ofdi-aromatic compounds. In an embodiment, the hydrodearylated liquidproduct stream 214 contains less than 20 wt. % of di-aromatic compounds.In an embodiment, the hydrodearylated liquid product stream 214 containsless than 10 wt. % of di-aromatic compounds. In an embodiment, thehydrodearylated liquid product stream 214 contains less than 1 wt. % ofdi-aromatic compounds. The hydrodearylated liquid product stream 214 issupplied to a second separator 216. Four streams exit the secondseparator 216: a benzene-containing stream 218, a toluene-containingstream 220, a C₈-containing stream 222, and a bottoms C₉₊ stream 224. Inan embodiment, the benzene-containing stream 218 contains less than 30wt. % of benzene. In another embodiment, the benzene-containing stream218 contains less than 20 wt. % of benzene. In another embodiment, thebenzene-containing stream 218 contains less than 10 wt. % of benzene. Inanother embodiment, the benzene-containing stream 218 contains less than5 wt. % of benzene. The toluene-containing stream 220 can be directed toa transalkylation reactor as a feed stream. In the transalkylationreactor, the toluene is combined with a C₉₊ stream to produce alkylmono-aromatic compounds. In an embodiment, the toluene-containing stream220 contains less than 30 wt. % of toluene. In another embodiment, thetoluene-containing stream 220 contains less than 20 wt. % of toluene. Inanother embodiment, the toluene-containing stream 220 contains less than15 wt. % of toluene. In another embodiment, the toluene-containingstream 220 contains less than 10 wt. % of toluene. The C₈-containingstream 222 is directed to the p-xylene production unit. In anembodiment, the C₈-containing stream 222 contains less than 30 wt. % ofC₈ compounds, such as xylene and ethylbenzene. In another embodiment,the C₈-containing stream 222 contains less than 20 wt. % of these C₈compounds. In another embodiment, the C₈-containing stream 222 containsless than 10 wt. % of these C₈ compounds. The C₉₊ stream 224 can besupplied as part of a feed stream 226 to a transalkylation unit. In anembodiment, the C₉₊ stream 224 is combined with the overhead stream 208containing C₉ and C₁₀ compounds and supplied as part of a feed stream226 to the transalkylation unit.

In an embodiment 300 as described in FIG. 3, the aromatic bottoms streamfrom an aromatic recovery complex is sent to a first separator 302. Twostreams exit the first separator 302: an overhead stream 304 containingC₉ and C₁₀ compounds and a bottoms stream 306 containing C₁₁₊ compounds.In an embodiment, the overhead stream 304 contains about 50-99 wt. % ofthe C₉ and C₁₀ compounds. In another embodiment, the overhead stream 304contains about 60-99 wt. % of the C₉ and C₁₀ compounds. In anembodiment, the overhead stream 304 contains about 80-99 wt. % of the C₉and C₁₀ compounds. For example, simulated distillation data indicatedthat the overhead stream 304 contains about 90-99 wt. % of the C₉ andC₁₀ compounds.

In an embodiment, the overhead stream 304 containing C₉ and C₁₀compounds can be supplied as part of a feed stream 320 to atransalkylation unit. The bottoms stream 306 containing C₁₁₊ compoundsis directed to a hydrodearylation unit 308 for processing into ahydrodearylated liquid product stream 310. In an embodiment, the bottomsstream 306 contains about 5-99 wt. % of C₁₁₊ compounds. In anotherembodiment, the bottoms stream 306 contains about 30-99 wt. % of C₁₁₊compounds. In an embodiment, the bottoms stream 306 contains about 80-99wt. % of C₁₁₊ compounds. The hydrodearylated liquid product stream 310is sent to a second separator 312. In an embodiment, the hydrodearylatedliquid product stream 310 contains about 10 wt. % of alkyl mono-aromaticcompounds. In an embodiment, the hydrodearylated liquid product stream310 contains about 20 wt. % of alkyl mono-aromatic compounds. In anembodiment, the hydrodearylated liquid product stream 310 contains about40 wt. % of alkyl mono-aromatic compounds. In an embodiment, thehydrodearylated liquid product stream 310 contains about 50 wt. % ofalkyl mono-aromatic compounds. In an embodiment, the hydrodearylatedliquid product stream 310 contains about 70 wt. % of alkyl mono-aromaticcompounds. In an embodiment, the hydrodearylated liquid product stream310 contains about 90 wt. % of alkyl mono-aromatic compounds. In anembodiment, the hydrodearylated liquid product stream 310 contains lessthan 70 wt. % of di-aromatic compounds. In an embodiment, thehydrodearylated liquid product stream 310 contains less than 40 wt. % ofdi-aromatic compounds. In an embodiment, the hydrodearylated liquidproduct stream 310 contains less than 20 wt. % of di-aromatic compounds.In an embodiment, the hydrodearylated liquid product stream 310 containsless than 10 wt. % of di-aromatic compounds. In an embodiment, thehydrodearylated liquid product stream 310 contains less than 1 wt. % ofdi-aromatic compounds.

Four streams exit the second separator 312: a benzene-containing stream314, a first toluene-containing stream 316, a first C₈-containing stream318, and a bottoms C₉₊ stream 320. In an embodiment, thebenzene-containing stream 314 contains less than 30 wt. % of benzene. Inanother embodiment, the benzene-containing stream 314 contains less than20 wt. % of benzene. In another embodiment, the benzene-containingstream 314 contains less than 10 wt. % of benzene. In anotherembodiment, the benzene-containing stream 314 contains less than 5 wt. %of benzene. In an embodiment, the first toluene-containing stream 316contains less than 30 wt. % of toluene. In another embodiment, the firsttoluene-containing stream 316 contains less than 20 wt. % of toluene. Inanother embodiment, the first toluene-containing stream 316 containsless than 15 wt. % of toluene. In another embodiment, the firsttoluene-containing stream 316 contains less than 10 wt. % of toluene.

In an embodiment, the first C₈-containing stream 318 contains less than30 wt. % of C₈ compounds, such as xylene and ethylbenzene. In anotherembodiment, the first C₈-containing stream 318 contains less than 20 wt.% of these C₈ compounds. In another embodiment, the first C₈-containingstream 318 contains less than 10 wt. % of these C₈ compounds.

In an embodiment, the bottoms C₉₊ stream is supplied as part of a feedstream 320 to a transalkylation unit. The benzene-containing stream 314is sent to a third separator 322. Two streams exit the third separator322: a benzene-enriched stream 324 that is directed to a transalkylationreactor, and a second toluene-containing stream 326 that is directed toa fourth separator 328, either as a separate feed stream or as a mixturewith the first toluene-containing stream 316. The firsttoluene-containing stream 316 can be supplied independently to thefourth separator 328. Two streams exit the fourth separator 328: atoluene-enriched stream 330 that is directed to a transalkylationreactor, and a second C₈-containing stream 332 that is directed to afifth separator 334, either as a separate feed stream or as a mixturewith the first C₈-rich stream 318. The first C₈-rich stream 318 can besupplied independently to the fifth separator 334. Two streams exit thefifth separator 334: a C₈-rich stream 336 that is directed to a p-xyleneproduction unit, and a C₉₊-containing stream 338 that is directed to thetransalkylation unit, either as a separate feed stream or as a mixturewith the bottoms C₉₊ stream 320. In an embodiment, the C₉₊-containingstream 338 is combined with the overhead stream 304 containing C₉ andC₁₀ compounds from the first separator 302 and supplied as a feed stream340 to the transalkylation unit. In another embodiment, the overheadstream 304 containing C₉ and C₁₀ compounds from the first separator 302,the bottoms C₉₊ stream 320 from the second separator 312, and theC₉₊-containing stream 338 from the fifth separator 334 are combined andsupplied as a feed stream 340 to a transalkylation unit. In anotherembodiment, each of these streams can be separately supplied to thefirst transalkylation unit.

Described here is a method and a system used for aromatictransalkylation to ethylbenzene and xylenes. In an embodiment 400 asdescribed in FIG. 4, the aromatic bottoms stream from an aromaticrecovery complex is sent to a hydrodearylation unit 402. Thehydrodearylated liquid product stream 404, exiting from thehydrodearylation unit 402, may also contain benzene, toluene and C₈compounds, along with C₉₊ alkyl aromatics. The hydrodearylated liquidproduct stream 404 is mixed with a benzene-containing stream 406 to forma feed stream 408. The feed stream 408 is supplied to a transalkylationreactor 410 either with or without an additional hydrogen stream 412.The feed stream 408 in the presence of a catalyst is converted to afirst product stream 414 containing benzene, C₈₊ aromatics includingethylbenzene and xylenes, and toluene. The first product stream 414 fromthe transalkylation reactor is directed to a first separation column416. The first product stream 414 is separated into three fractions: afirst overhead stream 418 containing benzene, a first bottoms stream 420containing C₈₊ aromatics including ethylbenzene and xylenes, and aside-cut stream 422 containing toluene. The overhead stream 418 isrecycled to the first transalkylation unit after benzene is removed viastream 424. The first bottoms stream 420 of C₈₊ aromatics, includingethylbenzene and xylenes, from the first separation column 416 isdirected to a second separation column 426. Two streams are recoveredfrom this second separation column 426: a second overhead stream 428 ofethylbenzene and xylenes, which is directed to a para-xylene unit 430 toproduce a para-xylene-rich stream 432, and a second bottoms stream 434of C₉₊ alkylaromatics. The side-cut stream 422 from the first separationcolumn 416 is supplied as part of a feed stream 436 to a thirdseparation column 438 after additional toluene is added or removed (notshown in FIG. 4). Toluene is normally recycled to extinction by reactingwith C₉ and C₁₀ to produce benzene and C₈. If there is a decrease orlack of toluene in the system, make-up toluene may be required. If thereis a decrease or lack of C₉/C₁₀, the amount of toluene can beproportionately reduced to make the stoichiometry. Certain marketconditions may influence the removal of toluene from the system. Theside-cut stream 422 is mixed with the second bottoms stream 434 of C₉₊alkylaromatics to form a combined feed stream 436 that is supplied tothe third separation column 438. Two streams are recovered from thisthird separation column 438: a third bottoms stream 440 of C₁₁₊alkylaromatics and an overhead stream 442 of C₉ and C₁₀ alkylaromaticsand lighter compounds (including C₇ alkylaromatics) directed to thetransalkylation unit 410. In certain embodiments, the unconvertedproducts can be recycled to the hydrodearylation unit 402 (not shown inFIG. 4).

Described here are processes and systems to fractionate thereject/bottoms stream of a xylene re-run column and to upgrade the fueloil components (heavy fraction) to petrochemical feedstock. Alsodescribed are embodiments to upgrade the as-received reject/bottomsstream from the xylene re-run column. The C₉₊ stream from a xylenere-run column is fractionated to remove C₉ and C₁₀, leaving a C₁₁₊stream, which is considered as a low-value fuel oil stream. The C₉ andC₁₀ stream is directed to a TA/TDP process unit to be processed to yieldincreased quantities of C₈ that can be further processed downstream toyield para-xylene. The C₁₁₊ fuel oil stream is subjected tohydrodearylation. The unconverted C₁₁₊ (mainly condensed diaromatics)stream is directed as fuel oil (approximately 25 wt. % of the originalfuel oil stream). The methods and systems disclosed here allow alow-value fuel oil stream to be upgraded into petrochemical feedstock.Approximately 75% of the fuel oil is converted to isomer grade mixedxylenes.

EXAMPLES

A couple of methods and systems for integration of a hydrodearylationprocess with a transalkylation process are illustrated here. While theparticular example provided below is for a stream containing C₉₊compounds, the methods and systems for integration of a hydrodearylationprocess with a transalkylation process can utilize a C₁₁₊ feed.

Example 1

About 7.97 kilograms of an aromatic bottoms fraction, derived from anon-fractionated C₉₊ feed, was distilled using a lab-scale true boilingpoint distillation column with 15 or more theoretical plate using theASTM D2892 method. The feed stream contains about 83 weight percent (wt.%) of a gasoline fraction (compounds with a boiling point ranging from36° C. to 180° C.) and about 17 wt. % of a residue fraction (compoundswith a boiling point above 180° C.).

Properties and composition of the feed stream are shown in Tables 1 and2.

TABLE 1 Feedstock Aromatics Gasoline Residue Property Bottoms FractionFraction Density 0.8834 0.8762 0.9181 Octane Number Not applicable 108Not applicable ASTM D2799

TABLE 2 Boiling Point, Boiling Point, Boiling Point, ° C. ° C. ° C.(Feedstock Aromatics (Gasoline (Residue Property Bottoms) Fraction)Fraction) Initial Boiling 153 154 163 Point 10 wt. % 163 164 190 30 wt.% 166 166 202 50 wt. % 172 171 231 70 wt. % 175 174 289 90 wt. % 191 183324 Final Boiling 337 204 359 point

In an example of a hydrodearylation process, a feedstock consisting of anon-fractionated xylene rerun column bottoms stream with the abovedescribed properties was treated in a hydrodearylation reaction zonecontaining a catalyst having nickel and molybdenum with ultrastableY-type (USY) zeolite on a silica-alumina support operated athydrodearylation conditions including a temperature ranging from 280 to340° C., at a hydrogen partial pressure of 15 or 30 bar, a liquid hourlyspace velocity of 1.7 hr⁻¹. Feed and hydrodearylated liquid productcompositions, as analyzed by two-dimensional gas chromatography, areprovided in Table 3.

TABLE 3 Run Temperature Pressure MA NMA MN DN P NDA DA TrA # ° C. BarWt. % Wt. % Wt. % Wt. % Wt. % Wt. % Wt. % Wt. % Feed 0 0 92.28 1.82 0.150.12 0.37 0.59 4.34 0.33 1 340 30 91.67 2.91 2.1 0.43 0.94 0.43 1.380.15 3 320 30 92.95 3.04 1.56 0.33 0.37 0.45 1.16 0.13 5 300 30 92.983.13 1.33 0.29 0.34 0.51 1.3 0.13 7 280 30 93.2 3.1 0.95 0.23 0.3 0.541.55 0.14 15 340 15 93.47 2.38 0.46 0.17 0.55 0.59 2.13 0.26 17 320 1593.69 2.15 0.34 0.1 0.4 0.72 2.34 0.26 19 300 15 93.73 2.1 0.29 0.080.35 0.71 2.46 0.29 21 280 15 93.63 2.09 0.27 0.08 0.33 0.77 2.54 0.28Key for Table 2—MA: Mono Aromatics; NMA: Naphtheno Mono Aromatics; MN:Mono-Naphthenes; DN: Di-naphthenes; P: Paraffins; NDA: Naphtheno DiAromatics; DA: Diaromatics; and TrA: Tri Aromatics

For example, subjecting the feed to hydrodearylation conditions in thepresence of the catalyst and hydrogen at 320° C. and 30 bar, there is anapproximately 75% reduction in diaromatic content. The decrease in thediaromatic content demonstrates that hydrodearylation has occurred andthe low-value heavy components of the stream have been upgraded tohigher value components. The technology also takes a low-value fuel oilfrom an aromatic bottoms/reject stream from an aromatic complex andupgrades the fuel oil to petrochemical feedstock.

Ranges may be expressed herein as from about one particular value and toabout another particular value. When such a range is expressed, it is tobe understood that another embodiment is from the one particular valueand/or to the other particular value, along with all combinations withinsaid range. Where the range of values is described or referenced here,the interval encompasses each intervening value between the upper limitand the lower limit as well as the upper limit and the lower limit andincludes smaller ranges of the interval subject to any specificexclusion provided. Where a method comprising two or more defined stepsis recited or referenced herein, the defined steps can be carried out inany order or simultaneously except where the context excludes thatpossibility. While various embodiments have been described in detail forthe purpose of illustration, they are not to be construed as limiting,but are intended to cover all the changes and modifications within thespirit and scope thereof

What is claimed is:
 1. A system for conversion of alkyl-bridgednon-condensed alkyl multi-aromatic compounds to alkyl mono-aromaticcompounds, the system comprising: a first separator adapted to receive afeed stream containing one or more of heavy alkyl aromatic compounds andone or more alkyl-bridged non-condensed alkyl multi-aromatic compoundshaving at least two benzene rings connected by an alkyl bridge groupwith at least two carbons and the benzene rings being connected todifferent carbons of the alkyl bridge group, and produces a firstproduct stream containing C₉ and C₁₀ compounds and a second productstream containing one or more of heavy alkyl aromatic compounds andalkyl-bridged non-condensed alkyl multi-aromatic compounds; ahydrodearylation reactor fluidly coupled to the first separator andadapted to receive a hydrogen stream and the second product stream andto produce a third product stream in presence of a catalyst, the thirdproduct stream containing one or more alkyl mono-aromatic compounds; anda second separator fluidly coupled to the hydrodearylation reactor andadapted to receive the third product stream and to produce abenzene-containing stream, a toluene-containing stream, a C₈-richstream, and a bottoms C₉₊ stream, the system adapted to combine thefirst product stream containing C₉ and C₁₀ compounds from the firstseparator and the bottoms C₉₊ stream from the second separator.
 2. Thesystem of claim 1, further comprising: a transalkylation/toluenedisproportionation unit fluidly coupled to the second separator andadapted to receive the first product stream and one or more of thebenzene-containing stream, the toluene-containing stream, and thebottoms C₉₊ stream, and to produce alkyl mono-aromatic compounds.
 3. Thesystem of claim 1, further comprising: a para-xylene unit fluidlycoupled to the second separator and adapted to receive the C₈-richstream and to produce a para-xylene-rich stream.
 4. The system of claim1, further comprising: a third separator fluidly coupled to the secondseparator and adapted to receive the benzene-containing stream andadapted to separate a benzene-enriched stream from toluene.
 5. Thesystem of claim 4, further comprising: a fourth separator fluidlycoupled to the second separator and the third separator, the fourthseparator adapted to receive the toluene-containing stream from thesecond separator and adapted to receive toluene from the third separatorto separate a toluene-enriched stream from C₈₊ compounds.
 6. The systemof claim 5, further comprising: a fifth separator fluidly coupled to thesecond separator and the fourth separator, the fifth separator adaptedto receive the C₈-rich stream from the second separator and adapted toreceive C₈₊ compounds from the fourth separator to separate aC₈-enriched para-xylene production stream from C₉₊ compounds.
 7. Thesystem of claim 1, wherein the feed stream is fluidly coupled to axylene rerun column of an aromatic recovery process.
 8. The system ofclaim 1, wherein the feed stream is supplied directly to the firstseparator from a xylene rerun column of an aromatic recovery process. 9.The system of claim 1, wherein a catalyst bed comprising catalyst in thehydrodearylation reactor is adapted to receive a portion of the hydrogenstream to quench the catalyst bed.
 10. The system of claim 9, whereinthe catalyst includes a support being at least one member of the groupconsisting of silica, alumina, titania, and combinations thereof, andfurther includes an acidic component being at least one member of thegroup consisting of amorphous silica-alumina, alumina, zeolite, andcombinations thereof.
 11. The system of claim 10, wherein the zeolite isone or more of or derived from FAU, *BEA, MOR, MFI, or MWW frameworktypes.
 12. The system of claim 9, wherein the catalyst includes an IUPACGroup 6-10 metal being at least one member of the group consisting ofiron, cobalt, nickel, molybdenum, tungsten, and combinations thereof.13. The system of claim 12, wherein an IUPAC Group 8-10 metal is 2 to 20percent by weight of the catalyst and an IUPAC Group 6 metal is 1 to 25percent by weight of the catalyst.
 14. The system of claim 1, whereinconditions in the hydrodearylation reactor include an operatingtemperature in the range of about 200 to 450° C.
 15. The system of claim1, wherein conditions in the hydrodearylation reactor include anoperating temperature in the range of about 250 to 450° C.
 16. Thesystem of claim 1, wherein conditions in the hydrodearylation reactorinclude an operating hydrogen partial pressure in the range of about 5bar gauge to 100 bar gauge.
 17. The system of claim 2, wherein thetransalkylation/toluene disproportionation unit is adapted to increasethe production of para-xylene.
 18. The system of claim 9, wherein thecatalyst in the catalyst bed does not comprise a metal.
 19. The systemof claim 9, wherein the catalyst in the catalyst bed does not comprisean IUPAC Group 6-10 metal.
 20. The system of claim 9, wherein thecatalyst bed comprises a catalyst support material and a binder operableto function as the catalyst without an added catalytic IUPAC Group 6-10metal.
 21. The system of claim 20, wherein the catalyst support materialcomprises a zeolitic material and the binder comprises alumina.
 22. Thesystem of claim 9, wherein an IUPAC Group 8-10 metal is 1 to 20 percentby weight of the catalyst, without an IUPAC Group 6 metal.
 23. Thesystem of claim 9, wherein an IUPAC Group 6 metal is 1 to 25 percent byweight of the catalyst, without an IUPAC Group 8-10 metal.